CN1199827A - Turbine/motor (generator) driven booster compressor - Google Patents

Turbine/motor (generator) driven booster compressor Download PDF

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Publication number
CN1199827A
CN1199827A CN98108939A CN98108939A CN1199827A CN 1199827 A CN1199827 A CN 1199827A CN 98108939 A CN98108939 A CN 98108939A CN 98108939 A CN98108939 A CN 98108939A CN 1199827 A CN1199827 A CN 1199827A
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Prior art keywords
turbine
compressor
nitrogen
stream
gas
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CN98108939A
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CN1138961C (en
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N·T·纳诺弗
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Praxair Technology Inc
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Praxair Technology Inc
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
    • F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
    • F01D15/12—Combinations with mechanical gearing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/04—Gas-turbine plants characterised by the use of combustion products as the working fluid having a turbine driving a compressor
    • F02C3/107—Gas-turbine plants characterised by the use of combustion products as the working fluid having a turbine driving a compressor with two or more rotors connected by power transmission
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B11/00—Compression machines, plants or systems, using turbines, e.g. gas turbines
    • F25B11/02—Compression machines, plants or systems, using turbines, e.g. gas turbines as expanders
    • F25B11/04—Compression machines, plants or systems, using turbines, e.g. gas turbines as expanders centrifugal type
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
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    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04133—Electrical motor as the prime mechanical driver
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    • F25J3/04139—Combination of different types of drivers mechanically coupled to the same compressor, possibly split on multiple compressor casings
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    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/044—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a single pressure main column system only
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
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    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream

Abstract

A compressor assembly for cryogenic gas separation wherein the assembly comprises a compressor, an expansion turbine and an electric motor integrally connected via a gear drive, and processes for using the compressor assembly.

Description

The booster compressor that turbine/motor machine (generator) drives
The present invention relates to the booster compressor that a kind of turbine/motor machine (generator) drives, in more detail, relate to a kind of combined unit that comprises by the booster compressor that cryogenic expansion turbine drove of a motor/generator power-assisted, and a kind of method of using this device.
In the past, because the selling at exorbitant prices of generator and relevant hardware, power is lower than 100 horsepowers seldom use in the production of blowing off of turbine.Many nitrogen (or oxygen) manufacturing mechanism has used a product compressor to improve product pressure according to user's technical requirements.On the other hand, there is not the product compressor in some nitrogen manufacturing mechanism (expanding) and be designed to can be in higher total pressure (it is by the decision of the needed pressure of product nitrogen) work down with waste material.This waste material bloating plant requires bigger energy, and the Economy of this equipment work is relatively poor.But, since with by saving the saving of the relevant capital investment of product compressor, it is rational that this poor efficiency has been proved to be.In general, the low temperature equipment of blowing off has the refrigeration that can control oneself to produce expander (turbine) is comparatively ideal.
For gas generation equipment is used for liquid production, preferably increase the size of turbine, correspondingly improve production process then.Generally, the production engineer can not increase the size of this turbine that has nothing to do with other production requirements.Therefore, the productivity of the quantity of the liquid of being produced and a device fabrication gas product usually (particularly in ambient temperature the very high date) can be restricted, and part is because the restriction of refrigeration.Therefore, it will be favourable adjusting the refrigerating capacity that is produced according to the requirement of a particular system.But it is unpractical adjusting refrigerating capacity and don't influence production process by the change turbine power, because this device is non-existent.
Just can improve the small-sized extremely efficient of medium-sized gas generation equipment as long as turbine power is used in the miscellaneous part (for example driving a booster compressor that is used for compressed products stream or feeding air itself) of equipment.The problem that past exists also has one and how to make the speed of turbine and compressor stage and the problem that power is complementary except capital investment.The running parameter of booster compressor comprises that pressure (head), flow and power all pass through (compression) accordingly stream and requires (or product stream or feeding air stream) to manage.Efficiency operation has determined the size and the optimum speed thereof of compressor usually.The technical requirements of these booster compressors and the operating head of turbine, flow and power requirements (they depend on other production purpose) are irrelevant and do not get in touch.
Turbine and compressor all must be allowed to turn round to reach the work of peak efficiency under its optimum speed.The speed of turbine and compressor and power are normally unmatched.In the past, people at first determine the size of turbine, adjust production process then and make pressurized machine center on turbine to fix size.Usually to take into account one or several procedure parameter, as flow, speed and efficient etc.Loading with generator under the situation of turbine, capital investment and operating cost play a decisive role in production is blown off in improvement.As a result, think always that traditionally it is uneconomic that turbine power is lower than 100 horsepowers of recovery, thereby pass into disuse.
As mentioned above, to medium size installations, turbine power is not utilized but has discarded in heat-radiation loop small-sized.If this power be used to Driven Compressor with energy recovery in produce, do like this and usually damage compressor performance, because the power of turbine and compressor and speed seldom can be mated.With of the load of a generator as turbine, though feasible economically, but still not as directly more effective with compressor.
Yet, the claimant knows the technology creation of also not describing content of the present invention at present, that is, cryogenic turbo that has a motor/generator and one-level (or what) compressor becomes a device by a tool gear box combination, thereby can all provide best effort to cryogenic turbo and compressor.It is unpractical on base load air compressor or the gear-box for example that cryogenic turbo is installed in warm end equipment, because the route of cryogenic turbo pipeline and insulation are set in or are close to this warm end equipment place many technical difficulties is arranged.In fact the latter is usually located at and installs the crogenic box of turbine pipeline and all cryogenic pipings at a distance of a distance.
The All aspects of that prior art relates to relevant expander design and uses.For example the cryogenic turbo of turbine of the compressor loads of using in the temperature production industry (Compander) and generator loading all is known in the art.People know that Compander can be used for producing low-pressure gas oxygen and/or nitrogen product in the equipment of blowing off.For example in U. S. Patent 5268328, motor and one is warm to produce that air turbine is combined to come Driven Compressor.
U. S. Patent 4817393 has proposed driving a small-sized warm end air compressor or driving the gap that does not almost have between the generator on the cost with this air horsepower output.The increment compression that U. S. Patent 4769055 has proposed to obtain at warm end compressor is a very economical, because driving power is " freedom " and capital investment Compander is sent the capital investment of expander of other devices of power and almost do not had what gap with having some absorptions.
An object of the present invention is to provide a kind of composite set of the booster compressor that is driven by the cryogenic turbo expander of a motor/generator power-assisted, this device can use in the temperature production circulation effectively.
Another object of the present invention is to confirm this temperature production circulation, can use this booster compressor that is driven by the turbine expander of motor/generator power-assisted cheaply effectively, and its efficient is not second to prior art.
Another purpose of the present invention provides a kind of reliable and firm cryogenic turbo expander, and this expander only needs lower capital investment and lower maintenance expenses.
A further object of the present invention provides a kind of turbine expander that can use in the equipment of production oxygen that makes air separation by cryogenic rectification and/or nitrogen and circulation.
Another object of the present invention be from one cheaply booster compressor increase refrigeration production, but different with other manufacturing mechanism be size (power) onrelevant with turbine.
The present invention is a kind of gas compressing apparatus that is used for refrigeration system.This device comprises a motor/generator, a compressor and a turboexpander, and they connect into an integral body by a gear drive.This turboexpander has a turbine inlet and a turbine outlet, makes the operating temperature of this compression set in the turbine inlet be lower than about 250 ° of K.The operating temperature of turbine outlet is lower than about 150 ° of K, is preferably lower than 100 ° of K.This refrigeration system can provide refrigeration, so that with at least a gas componant liquefaction, perhaps be used for from the gas separation of at least a gaseous mixture separating out at least one gas componant.Control gear regulate at least a portion gas sequentially by compressor to turbine.
The invention still further relates to a kind of refrigeration method, this method comprises the steps: to make a kind of gaseous mixture to be separated at least a gas products; A part of gas products is entered in the turbine of compression set, and this compression set has a turbine, a compressor and a motor/generator, and they connect into an integral body by a gear drive.This turbine has a turbine inlet and a turbine outlet, makes that the operating temperature in the turbine inlet is lower than about 250 ° of K.Operating temperature in turbine outlet is lower than about 150 ° of K, is preferably lower than 100 ° of K.At least a portion gaseous mixture occurs as at least a compressed gas mixtures by compressor.This cryogenic rectification tower system can comprise a single tower and a last condenser, and wherein at least a portion gaseous mixture occurs by the gas products of this single tower as at least a purification.This Purge gas product comprises that a kind of purity is greater than about 95% height concentrated gas products and the medium concentrated gas products of a kind of purity between about 55% to about 75%.This cryogenic rectification tower system can comprise a Xia Ta, a Shang Ta and a main condenser, and wherein the gas products of at least a purification passes through compressor from condenser, and then in expander.
To most preferred embodiment and the description of the drawings, other purposes of the present invention, characteristics and advantage will appear in those of ordinary skill in the art's brains, in the accompanying drawing by following:
Fig. 1 is the assembled cross-sectional view of Fig of the booster compressor of turbine/motor machine reinforcing;
Fig. 2 is the general flow chart with waste material expansion nitrogen equipment of product compressor;
Fig. 3 is the general flow chart of waste material expansion nitrogen equipment with booster compressor of part feeding air stream;
Fig. 4 is the flow chart with gas oxygen equipment of part liquid nitrogen/oxygen production; And
Fig. 5 is the sketch of a shaft seal.
Describe the present invention below with reference to accompanying drawings.Fig. 1 is by the motor/generator reinforcing, the assembled cross-sectional view of Fig of the booster compressor that cryogenic turbo drives.Turbine 101, compressor 102 and motor/generator 103 all are connected on the gear-box 104.This turbine is made up of support 105 and turbine shroud 106.The rotor 107 of turbine 101 rotates in turbine bearing 108, and those bearing centerings also are installed in the gear-box 104.Inflating end axle envelope 109 is held and is centered in the turbine support 105, and this support itself is centered in the gear-box 104.
The gear-box along continuous straight runs is split, so that the replacing of single parts and maintenance and can not disturb the miscellaneous part of this gear-box.After gear box cover is taken off, just can from turbine shroud and gear-box, take out the turbine support and can not disturb crogenic box insulation.The gear-box that turbine of the present invention, booster compressor and motor/generator be installed preferably be positioned at very near and with " crogenic box " adjacent position on, promptly Fig. 1 is seen in the people place of being ready to place turbine itself usually.
This being configured in is more desirable economically because it utilized " common " turbine stage and since turbine shroud made and enter the ducted possible heat leak loss of turbine and " cold low temperature " thereof and reduce to minimum to carry out thermal insulation by the thermal insulation of perlite or some other types in crogenic box by " submergence ".Preferably booster compressor be placed near crogenic box and with the position adjacent of turbine own.
Booster compressor level and motor/generator are with all warm (turbine and crogenic box) opposite sides of holding (booster compressor) pipelines to be placed on gear-box.The gear-box along continuous straight runs is split, so that separately near each critical piece, i.e. and turbine, compressor, motor or gear and bearing housing.Therefore, by taking off gear box cover, the operator can be easily near and take out any one in these parts individually and can not influence other two parts.
Turbine is connected with compressor by gear transmission.Operating temperature in the turbine ingress is less than about 250 ° of K.By after the turbine, the operating temperature at the turbine outlet place is less than about 150 ° of K, preferably is less than about 100 ° of K in combustion gas.
Low-temperature expansion device thermal protection shield 110 is in the warm sector and the turbine support between the cold expander gear 111 of gear-box.So it must do two reasons like this: the first, will jeopardize freezing of mechanical function in order to protect the unlikely generation of lubricant oil in bearing; And the second, in order to prevent heat leakage to producing in the fluid, this will unnecessarily reduce the efficient and the performance of expander.
Expander housing 106 provides and has been used for producing the device that fluid imports turbine expander described herein and discharges from this expander.Also can utilize by the additional compressor stage that motor drive unit 114 or other mechanisms drive.Turbine 101 is equipped with compressor impeller 112 and compressor stage 102 by the gear train 113 that is arranged in gear-box 104.Another gear 114 that turbine rotor is connected on the motor/generator 103 will provide additional power input or absorb unnecessary turbine power for compressor according to production requirement.
If the turbine of Driven Compressor level is by gear transmission and a motor parallel job, as shown in Figure 1, we just can save the capital investment of equipment and can also improve the efficient of the energy of production process.Higher by on the turbine an of low temperature (or any production process), there being the last compressor stage of tipping just to install the efficient of an independent generator than beginning, because this is a kind of more direct method of receiving the primary power input that flows back to from the fluid that expands.It has avoided the poor efficiency that links mutually with energy and the transformation of energy between the electric energy from cryogenic turbo.
Tooth changes transmission device can make turbine and compressor all work independently under its corresponding optimum speed.Asynchronous motor/generator can automatically compensate the difference power of this two-stage, if promptly the power that produces of turbine is less than the desired power of compressor, motor will be supplied with this difference power so.On the other hand, when having surplus power, motor will (difference only be several commentaries on classics of per minute, RPM), thereby surplus power is converted to electric energy as generator operation.These are all finished automatically, do not need the control that adds.
In the time of in the equipment that is applied to a product compressor of needs, this device can be exempted the capital investment of an additional booster compressor, because the loading compressor of turbine just can be this product booster compressor.Herein fund is saved the cost of production that not only comprises this compressor hardware itself, also comprise all usually be independent of outside the product booster compressor with slide device, pipeline.Relevant expenses such as cooling (water), wire terminal, basis, controller.
This device can make compressor and turbine all can move under its optimum efficiency or the situation near its optimum efficiency independently.It can permission or compressor stage or turbine stage be in optimum speed and irrelevant with the mismatch performance number of these two rotors.Induction alternating current (AC) motor will be by as motor or generator operation and automatically compensate the difference power of these two rotors.
A control gear can make compression set move under optimum efficiency.This control gear can be used for regulating the pressure of at least a portion by the gas pipeline of turbine.This control gear can be a mechanical device for the usefulness Computer Processing known to the skilled craftsman of related domain.
This gas compressing apparatus can make equipment that refrigeration can be provided for the liquefaction of at least a gas componant and/or provide refrigeration for the gas separation that is separated at least a gas componant from least a gaseous mixture.
Fig. 2 shows an embodiment by a turboexpander of the present invention and a waste material expansion low temperature nitrogen production system that has a product compressor that motor/generator drove.It illustrates for illustrative purposes, thereby it can be used in any suitable cryogenic rectification equipment.It is useful especially in the production cycle of a waste material expansion cryogenic nitrogen.Being subjected to expanding from the waste streams of rectifying column produces refrigeration, the waste streams of this expansion with the feeding air indirect heat exchange mode of input process therefrom, thereby make the feeding air cooling and in the rectifying column system, form refrigeration and produce rectifying.The present invention has also redefined the Applicable scope of waste material expansion nitrogen manufacturing mechanism, because the energy consumption of their unit gas products is improved.Fig. 2 shows a kind of application example that uses a product booster compressor of the present invention and a motor/generator.This equipment does not have the product compressor traditionally, but the pressurized machine level of this motor of the present invention/turbine power-assisted can be used as the one-level in the multistage feeding air engine or only be used for compressing a part of feeding air stream, as shown in Figure 3.
Referring now to Fig. 2,, the gaseous mixture that contains nitrogen and oxygen is that feeding air 201 is compressed in base load feeding air compressor 202, passes main heat exchanger 203 then.In this main heat exchanger 203, this feeding air by compression by and the waste fluid that expands between hot heat exchange cooled off, this will be described in more detail hereinafter.This by compression and the feeding air that cooled off (impurity of high-boiling wherein for example water vapour and carbon dioxide is eliminated) enter a cryogenic rectification tower system as air-flow 205 then.
The cryogenic rectification tower system that is shown among Fig. 2 comprises single tower 206 and last condenser 208.Also can use though comprise the equipment of more than one tower, preferably this cryogenic rectification equipment includes only a tower.Tower 206 is preferably in per square inch and works in 40 pounds to 140 pounds absolute pressure (psia) scope.
This feeding air is separated into nitrogen stream 209 and stream of oxygen-enriched liquid 207 by cryogenic rectification in tower 206.Nitrogen stream is discharged from the top of tower 206, and it has the purity of about nitrogen 95% or more usually, and preferably its purity range extremely between about 99.9999% the nitrogen, perhaps has higher purity at about 98% nitrogen.The part 226 of nitrogen stream 209 enters in the condenser 208, and is subjected to condensation against stream of oxygen-enriched liquid therein, enters in the tower 206 as backflow 217 then.If desired, the part 220 of liquid nitrogen stream 217 can be used as liquid nitrogen product 218 recovery.The nitrogen gas concn scope that this has usually is from about 55% to about 75%, preferably from about 60% to about 70% stream of oxygen-enriched liquid is discharged from the bottom of tower 206 as stream of oxygen-enriched liquid 207, enters in the top condenser 208 and seethes with excitement therein by valve 234 step-downs and as liquid stream 227 and carry out condensation so that nitrogen is flowed 226.
The nitrogen stream 209 that is discharged from carries out indirect heat exchange by main heat exchanger 203 and feeding air and is subjected to the warm feeding air cooling that makes thus.After this, be compressed by the pressurized product compressor 260 that drives by motor 270 and low-temperature expansion device 213 by warm nitrogen stream 223, thereby form recuperable product high pressure nitrogen gas 224.
Nitrogenous waste liquid is taken discharge the last condenser 208 of system as liquid stream 212 from rectifying, the part of this liquid stream is by main heat exchanger 203 then, and then by turbine expander 213 be inflated its scope at 20 psia to a pressure between the atmospheric pressure.Expander 213 is connected with a motor with a nitrogen product compressor.In this direct-connected expander-compressor assembly, two devices all by or do not carry out mechanical connection by gearing, thereby the energy that extracts from the air-flow that expands is directly sent to by compression the product nitrogen gas by compressor by expander.Additional this low-temperature expansion device of motor with suitable framework and size drives the product compressor.This motor, expander and compressor mechanically are connected to each other by the gear train that is arranged in gear-box of the present invention.This configuration makes and reduces to minimum with the extraneoas loss and the capital cost of linking for compressor mutually by an intergrade (for example generating) from expander to the energy indirect communication.Waste liquid 212 by and drive expander 213, then this expander again the part Driven Compressor so that compressed products nitrogen.Simultaneously, the waste liquid of this expansion is owing to cooled off by turbine expander 213.
The waste liquid 214 of the expansion of being cooled off then carries out indirect heat exchange by main heat exchanger 203 and feeding air and is subjected to the warm feeding air cooling that makes simultaneously, thereby provides refrigeration and produce or carry out cryogenic rectification in low temperature distillation system with this feeding air.Then the warm waste liquid that is produced is discharged from main heat exchanger 203 and discarded as waste liquid stream 216.
Fig. 3 shows another certain embodiments of the waste material bloating plant with the gaseous mixture (being the feeding air stream) that partly contains nitrogen and oxygen, and this equipment is compressed by the booster compressor that turbine/motor machine of the present invention drives.It illustrates for illustrative purposes, thereby it can be used in any suitable cryogenic rectification equipment.
Referring now to Fig. 3,, only some feeding air stream 301 bypass is by the last level of base load air compressor 302.The bypass segment 340 of feeding air is subjected to the compression of booster compressor 350 and occurs with part 341, and the head pressure of winner's feeding air engine 302 is in the scope of 40 pounds to 140 pounds absolute pressures (psia) per square inch.The flow of the air-flow 340 of bypass segment is by being determined from the output of the useful horsepower of cryogenic turbo 313 and the effective rate of utilization of motor 370 that is used for a suitable frame size of this special-purpose.After reconfiguring, two strands of feeding air streams are by main heat exchanger 303.In main heat exchanger 303, this feeding air by compression is by being cooled off with the indirect heat exchange of the waster material fluid that expands, and this will be described in more detail hereinafter.This by compression and the feeding air that cooled off (impurity for example water vapour and carbon dioxide that it has also removed high-boiling) enter a cryogenic rectification tower system as air-flow 305 then.
The cryogenic rectification tower system that is shown among Fig. 3 comprises single tower 306 and last condenser 308.Also can use though comprise the equipment of more than one tower, preferably this cryogenic rectification equipment includes only a tower in practice of the present invention.Tower 306 is preferably in per square inch and works in 40 pounds to 140 pounds absolute pressure (psia) scope.
This feeding air is separated into nitrogen stream 309 and stream of oxygen-enriched liquid 307 by cryogenic rectification in tower 306.Nitrogen stream is discharged from the top of tower 306, and it has the purity of the nitrogen 95% or more usually, and preferably its purity range extremely between about 99.9999% the nitrogen, perhaps has higher purity at about 98% nitrogen.The part 326 of nitrogen stream 309 enters in the condenser 308, and is subjected to condensation against stream of oxygen-enriched liquid therein, enters in the tower 306 as backflow 317 then.If desired, the part 320 of liquid nitrogen stream 317 can be used as liquid nitrogen product 318 recovery.The nitrogen gas concn scope that this stream of oxygen-enriched liquid has usually is from about 55% to about 75%, preferably from about 60% to about 70%, it is discharged from the bottom of tower 306 as stream of oxygen-enriched liquid 307, enters in the top condenser 308 and seethes with excitement therein by valve 334 step-downs and as liquid stream 327 and carry out condensation so that nitrogen is flowed 326.
The nitrogen stream 309 that is discharged from carries out indirect heat exchange by main heat exchanger 303 and feeding air and is subjected to the warm feeding air cooling that makes thus.After this, can be reclaimed by warm nitrogen stream 323.
Nitrogenous waste liquid is discharged from the last condenser 308 of rectifying column system as liquid stream 312, the part of this liquid stream is by main heat exchanger 303 then, and then by turbine expander 313 be inflated its scope at 20psia to a pressure between the atmospheric pressure.Carrying out indirect heat exchange by main heat exchanger 303 and feeding air and be subjected to the warm feeding air that cooled off simultaneously by the be cooled waste liquid 314 that expands of expander 313, is that low temperature distillation system provides refrigeration to produce or carry out the cryogenic rectification of feeding air with this feeding air thus.Then the warm waste liquid that is produced is discharged from main heat exchanger 303 as waste liquid stream 316.
In this specific application as shown in Figure 3, the last level of base load air compressor 302 must be designed to stably and safely work, away from owing to partly reduce the place that main feeding air stream causes fluctuation.Therefore, this configuration can provide the power utilization of turbine and make the power reduction of main feeding compressor drive.Though be used for replenishing the capital investment that additional small size motor will increase this turbine a little of being somebody's turn to do of turbine, do still favourable economically like this.
Fig. 4 is a specific embodiment of the gaseous oxygen production cycle that illustrates for the purpose of illustration.The present invention can be used in any suitable cryogenic rectification equipment.It is particularly useful in oxygen production equipment, and this equipment or have last tower air expansion perhaps has plate rail formula tower nitrogen expansion as shown in Figure 4, and wherein the useless nitrogen stream from rectifying column is expanded so that produce refrigeration.Thereby the waste streams of this expansion makes the feeding air cooling with indirect heat exchange method through the feeding air of importing and provides refrigeration thus in the rectifying column system and produce rectifying.
In Fig. 4, this booster compressor level can be used for increasing effectively by the pressure (and energy) that improves this turbine airflow the cooling power of this turbine before turbine airflow expands in turbine.The motor of the appropriate size of installation in position will can be this operating mode secondary power (when being required like this) will be provided.
Referring now to Fig. 4,, the gaseous mixture that contains nitrogen and oxygen be feeding air 401 in base load feeding compressor 402 by compression, removal of contamination in advance in prepurifier 402 is then by main heat exchanger 404.In main heat exchanger 404, feeding air by compression is by being cooled off with product and other indirect heat exchanges of returning cold flow.The cold feeding air of this pressurized enters in the following tower 406 of cryogenic rectification tower system as air-flow 405 then.
The cryogenic rectification tower system that is shown among Fig. 4 comprises tower 406 down, last tower 415 and main condenser 411.Following tower 406 is preferably in per square inch and works in 40 pounds to 140 pounds absolute pressure (psia) scope.In following tower 406, the feeding air is separated into nitrogen stream 410 and stream of oxygen-enriched liquid 416 by cryogenic rectification.Part nitrogen stream 410 enters the top of main condenser 411 and is subjected to condensation against the liquid oxygen of the boiling of last tower therein, returns as the liquid nitrogen stream 412 that refluxes then to enter down in the tower 406.
Its contain nitrogen concentration usually the stream of oxygen-enriched liquid between 60% to 70% discharge from the bottom of tower 406 down as liquid stream 416, in heat exchanger 417, be cooled against product or useless nitrogen stream 419, reduced pressure and having entered in the tower 415 as liquid stream 418.Useless then nitrogen stream 419 is discharged as useless nitrogen stream 420 by heat exchanger 414,417 and 404.The range of working pressure of last tower is preferably in per square inch between 15 to 25 pounds of absolute pressures (psia).Gaseous oxygen product is discharged from main condenser liquid as air-flow 421, then in main heat exchanger 404 against the feeding air and by warm and discharge as gaseous oxygen product stream 422.
Nitrogen stream is discharged from the circuit high pressure vapor stream of main condenser 411 as air-flow 407.Being subjected to the warm of feeding air and in booster compressor 430, being compressed in the passage in the passage of main heat exchanger 404 then.After in another passage of main heat exchanger 404 compression and the heat of local precooling being emitted, this nitrogen stream is expanded in the expander 408 and is produced needed refrigeration with regard to entering, with the carrying out of maintenance distillation process.Then, the expansion waste liquid of the cooling stream other passage by main heat exchanger 404 carries out indirect heat exchange with the feeding air and is subjected to the warm feeding air cooling that makes simultaneously, thus generation or carry out cryogenic rectification.Then the hot nitrogen stream that is produced is discharged from main heat exchanger 404 as waste streams 409 and discarded.Turbine expander 408 is subjected to the assistance of motor/generator 440 when driving booster compressor 430.Booster compressor level herein can be used for mainly increasing effectively by the pressure (and energy) that improves this turbine airflow 407 cooling power of turbine before turbine airflow 407 expands in turbine.The motor of the appropriate size of installation in position will can be this operating mode secondary power (when being required like this) will be provided.The size of this turbine and pressurized machine level should be suitable for work under the maximum load (being pressure ratio).
The operation that reduces turbine power can keep its flow constant reaching fully when reducing the turbine inlet pressure.This can utilize the suction guide vane that is positioned at the booster compressor ingress to finish.The adjusting that sucks guide vane also will make the exhaust pressure of pressurized machine and the output power of turbine (generation refrigeration) simultaneously adjusted, not have a strong impact on and can not produce turbine flow and production cycle.
Another strand liquid nitrogen stream 413 is always discharged in liquid nitrogen (nitrogen condensation product) stream 412 and is introduced as refluxing in the cap of tower later on by the cooling of the part in heat exchanger 414 from returning of main condenser.This backflow for the top rectifying column of starting low pressure so that produce highly purified nitrogen and oxygen product is essential.
Secondary power to the cryogenic turbo expander can obtain from motor by the bootstrap (boot-strapped) by booster compressor before air-flow expands in this turbine expander.When needing, additional refrigeration can be provided immediately like this and production cycle can be do not influenced.If desired, a part of liquid nitrogen stream 412 can be used as liquid nitrogen product 424 and reclaims.Equally, a part of oxygen also can be used as liquid oxygen product 423 and reclaims from the liquid oxygen of the boiling of the bottom position that is arranged in tower 415.Usually, the oxygen purity that had of gaseous oxygen product stream 422 and liquid oxygen product 423 is all greater than 95%.Best, this contains oxygen purity and surpasses 99.5%.
Bearing lubricant moves by the expander shaft sealer to the temperature production fluid and stops by warm cushion seal gas is imported in the shaft sealing of expander end, as shown in Figure 5.The sealing device is any device that cushion seal gas can be contained in axle-peritrochanteric.Usually, can hold an axle envelope with labyrinth 550, a series of local compression can be set up along axle 507 in this labyrinth to be increased, thus stoped oiling agent from bearing 508 to the impeller 511 of turbine expander 501 flow and temperature production gas from expander impeller 511 flowing to bearing and gear-box 104.So effectively bearing and gear-box are kept apart with this lifes production fluid flow, guaranteed the reliably working of turbine expander thus and oil can not take place in bearing, freeze or give birth to the situation that production fluid flow is subjected to the bearing lubricant pollution.
Warm sealing gas is fed in the seal arrangement by supply valve 551 in 40 to 150 temperature range usually.Sealing gas is preferably identical with the life production fluid flow, and for example nitrogen or mistake are given air.For being reduced, expander efficient reduces to minimum, the quantity that flows into the warm sealing gas of high pressure in the expander housing can remain minimum by pressure regulator 552, promptly this gas is directed into living production fluid flow to inject the place a little more than a pressure producing flow stream pressure at it.Low pressure seal gas also can be set in to be similar to and infeed in this device under 15 pounds of manometer pressure (psig) per square inch by back pressure regulator 553.The sealing gas supply of this low pressure can guarantee to give birth to production fluid flow and can never be polluted by oil.Basically all sealing gas all infeed in the sealing device when turbine starts and cuts out.
As those of ordinary skill in the art was accessible, the sealing gas device was need to be only at the expander end place of cryogenic turbo expander rotor.Do not need sealing gas at another warm end of this turbine rotor and at arbitrary end of compressor stage rotor.But the circulation process gas of this compressor for example air or nitrogen can be by similar mazy type shaft sealing effusions between compressor impeller and compressor section bearing.
The present invention may be summarized as follows: in the advantage of economic aspect
For the small-sized gas apparatus (50 to 200 ton per day) of the product compressor that needs supercharging, the corresponding capital investment of this compressor (comprising slide device, pipeline, basis, cooling water, electrical connector, control gear etc.) is about 250,000 dollars.Secondly, also have turbine and deceleration loading device (compressor brake, oil brake or motor) thereof.
The booster compressor of turbine/motor machine/generator drive of the present invention can be that cost replaces the product compressor satisfactorily with the expensive slightly turbine of expense, can save all capital investments relevant with it thus.In this way, people at least every equipment (50 to 200 ton per day) can save 100,000 to 200,000 dollars and add in other savings of producing with concerned power.
Following example has illustrated economic benefit of the present invention:
Cryogenic oxygen/nitrogen the manufacturing mechanism of 100 tons of throughput will need the cryogenic turbo of the generation refrigeration of 50SHP (shaft horsepower) every day, this turbine with the rotational speed of approximate 10000RPM (rpm) to obtain peak efficiency.In addition, in order to improve the pressure of product nitrogen stream, for example bring up to 30psia (whenever flat inchpound absolute pressure), we will need the product nitrogen booster compressor of about 100SHP of a rotational speed with about 27000RPM (so that it moves) under optimum efficiency.Use cryogenic turbo of the present invention/electric motor driven booster compressor, we only need the motor of the shortcoming volume of the 50SHP of purchase between compressor horsepower demand and turbine power output value.
If there is not benefit of the present invention, people must buy 175SHP (it has exceeded 125SHP), because the not 100SHP of product compressor still that needs now to buy, but also to bear (under the situation of base load feeding air compressor) because the poor efficiency that two kinds of machineries are feeding air compressor and cryogenic turbo makes up the loss power (50SHP at the cryogenic turbo place has just become the 75SHP at base load air compression arbor place now) of the cryogenic turbo that causes.In addition, under latter event, also must bear the installation and operation expense of a whole new booster compressor, comprise the expense of aspects such as slide device, pipeline, basis, cooling water, electrical connector, control gear.
Use the present invention, people can save about 100,000 dollars fund, because the separate unit installation fee of the booster compressor that this is specific is about 150,000 dollars, the expense of this separate unit cryogenic turbo is about 100,000 dollars, and the higher expense of the booster compressor of turbine/motor machine/generator drive of the present invention is about 150,000 dollars.With 0.05 dollar of calculating in every watt hour, annual expense in running power cost method can be saved 50,000 dollars approximately again.
In order to realize above-mentioned economic benefits, this device need have the gear-box of a special use, so that make the process gas turbine, motor/generator and booster compressor are connected to each other.The gear-box that turbine of the present invention, booster compressor and motor/generator be installed preferably is positioned at very near " crogenic box " and is adjacent on the position that connects, and promptly people are ready the place of the turbine placed itself usually.
This being configured in is more desirable economically because it utilized " common " turbine stage and since turbine shroud by " submergence " in crogenic box and the thermal insulation by perlite or some other types make and enter turbine and (cold low temperature) ducted possible heat leak loss reduces to minimum.Booster compressor be placed near crogenic box and with the adjacent position of turbine with under reverse situation, if turbine is for example to be placed on and base load air source equipment or the adjacent position of certain other compressor, cold (low temperature) turbine airflow is transported to pipe in the warm end device of this equipment and compares, will be easy to and also comparatively worthwhile on expense.
Booster compressor level and motor/generator are with all warm (crogenic box) opposite sides of holding (booster compressor) pipelines to be placed on gear-box.The gear-box along continuous straight runs is split, so that separately near each parts in 3 critical pieces, i.e. turbine, compressor, motor or gear and bearing housing.Therefore, by taking off gear box cover, the operator can be easily near and take out any one in these parts separately and can not influence other two parts.
As mentioned above and as shown in Figure 4, this booster compressor level can be used for increasing effectively by the pressure that improves turbine airflow the cooling power of cryogenic turbo before turbine airflow expands in turbine.In this process, (in this turbine) air communication that expands is crossed a booster compressor level and is compressed, and it loads turbine again then.
Traditionally, in a typical gas apparatus, the production of liquid is regulated by changing turbine flow usually.But,, further increase turbine flow and will cause the remarkable reduction of yield and the bigger overall power loss of base load air compressor sometime.Production cycle that Here it is can not be made the key of more fluid products economically.
By turbine drives, the pressurized machine of motor power-assisted, secondary power (for example being used for improving the pressure of turbine airflow) are that motor and the booster compressor by normal size provides for of the present invention.In this case, the size of turbine and pressurized machine level is a load (being pressure ratio) with maximum and fixed.Additional power will provide by motor.
The operation that reduces turbine power can reach by reducing the turbine inlet pressure when keeping its flow quite stable.This can utilize the suction guide vane that is positioned at the booster compressor ingress to finish.The adjusting that sucks guide vane also makes the exhaust pressure of pressurized machine and the output power of turbine (producing refrigeration) obtain simultaneously adjusting, but can not have a strong impact on turbine flow and production cycle generation itself.
In the particular case of above-mentioned 100TPD equipment, the present invention is used to improve the inlet energy of the turbine airflow in this bootstrapping booster compressor automatically by the motor that is shown among Fig. 4, just can produce extra fluid product as long as buy this gas apparatus of secondary power of this motor like this.For example, inlet guide vance or other devices by booster compressor make the load that acts on the turbine be increased to 75SHP from 50SHP, and extra 4% product nitrogen just can be used as that liquid production is come out and can not influence production cycle itself.If there is not the booster compressor by turbine drives motor power-assisted of the present invention, this is difficult to finish.
The working efficiency of compressor stage and low-temperature expansion device level can be because of both being combined in the equipment and is suffered damage.It is suitable for the nitrogen manufacturing mechanism with waste material expansion or air expansion.In some applications, for example oxygen produce air separation equipment or or even less nitrogen manufacturing mechanism in, this equipment can obtain extra fluid product by the help (because auxiliary refrigerating) that utilizes motor.This equipment especially is fit to by utilizing waste material expansion or air expansion circuit low temperature distillation to make the nitrogen manufacturing mechanism of air separation.It also can be used in other the temperature production, for example hydrogen, natural-gas or need low production cost and the similar chemical products production of the expander of prior art performance and compressor stage combination.
By utilizing the booster compressor of cryogenic turbo drive motor of the present invention/generator power-assisted, can use cryogenic rectification to produce nitrogen or oxygen product with lower total operating cost (and the bigger capital investment loss of unlikely generation).In the feature of the present invention shown in one or more accompanying drawings just for convenience's sake, because each feature can combine with other features of the present invention.Those skilled in the art can recognize that other various embodiments and these embodiments should be included in the scope of these claims.

Claims (10)

1. gas compressing apparatus that is used for refrigeration system, this compression set comprises a motor/generator, a compressor and a turboexpander with a turbine inlet and a turbine outlet, wherein said compressor, turbine and motor/generator connect into an integral body by a gear drive and the operating temperature of described compression set in described turbine inlet is lower than about 250 ° of K.
2. compression set as claimed in claim 1 is characterized in that, refrigeration is provided in described system so that the liquefaction of at least a gas componant.
3. compression set as claimed in claim 1 is characterized in that described system provides refrigeration, is used for from the gas separation of at least a gaseous mixture separating out at least one gas componant.
4. compression set as claimed in claim 1 is characterized in that, this device comprises that one is used at least a portion gas sequentially by the delivery pipe of described compressor to described turbine.
5. refrigeration method comprises:
A) make a kind of gaseous mixture by a cryogenic rectification tower system, described mixture is separated into the product of at least a gas; And
B) a part of described gas products is entered in the turboexpander of a compression set, this compression set comprises a turbine, a compressor and a motor/generator, these parts connect into an integral body by a tool gear drive, wherein said turbine has a turbine inlet and a turbine outlet, and the operating temperature of described compression set in described turbine inlet is lower than about 250 ° of K.
6. method as claimed in claim 5 is characterized in that, this method also comprises the described gaseous mixture of at least a portion by described compressor, to discharge as at least a compressed gas mixtures.
7. method as claimed in claim 5, it is characterized in that, this method also comprises makes a part of described gaseous mixture by a feeding compressor by compression earlier, and then make this gaseous mixture by described compression set, and reconfiguring with this remainder from the described gaseous mixture of described feeding compressor from gaseous mixture that described device produced.
8. method as claimed in claim 5, it is characterized in that, described cryogenic rectification tower system comprises a single tower and a last condenser, and wherein the described gaseous mixture of at least a portion is discharged with the gas products as at least a purification by described single tower.
9. method as claimed in claim 5 is characterized in that, described cryogenic rectification tower system comprises a following tower, a Shang Ta and a main condenser, and wherein at least a gas products is by described compressor.
10. method as claimed in claim 5 is characterized in that, this method comprises:
A) make a kind of gaseous mixture that contains nitrogen and oxygen by a cryogenic rectification equipment that comprises a single tower, to discharge as at least a nitrogen stream and a kind of stream of oxygen-enriched liquid;
B) use described stream of oxygen-enriched liquid to carry out condensation, thereby give birth to a kind of liquid nitrogen stream, make a kind of nitrogen waste stream from described stream of oxygen-enriched liquid, discharge from described nitrogen miscarriage;
C) a part of described liquid nitrogen stream therefrom reclaims as a kind of liquid nitrogen product;
D) the described liquid nitrogen stream of another part is entered as backflow and carry out recirculation in the described tower;
E) make the compressor of the described nitrogen stream of another part by a compression set, this compression set comprises described compressor, a turbine expander and a motor/generator, these parts connect into an integral body by a gear drive, the inlet operating temperature of wherein said turbine is lower than about 250 ° of K, and wherein product nitrogen from wherein reclaiming; And
F) make the described nitrogen waste stream of at least a portion by described turbine expansion.
CNB981089399A 1997-05-19 1998-05-18 Turbine/motor (generator) driven booster compressor Expired - Fee Related CN1138961C (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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CN112066643A (en) * 2020-07-28 2020-12-11 上海加力气体有限公司 Air separation process with reduced energy consumption

Families Citing this family (64)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5901579A (en) * 1998-04-03 1999-05-11 Praxair Technology, Inc. Cryogenic air separation system with integrated machine compression
EP1030350A4 (en) * 1998-07-08 2007-10-31 Taiyo Nippon Sanso Corp System and method for producing and supplying highly clean dry air
US6393865B1 (en) * 2000-09-27 2002-05-28 Air Products And Chemicals, Inc. Combined service main air/product compressor
US6484533B1 (en) 2000-11-02 2002-11-26 Air Products And Chemicals, Inc. Method and apparatus for the production of a liquid cryogen
FR2860576A1 (en) * 2003-10-01 2005-04-08 Air Liquide APPARATUS AND METHOD FOR SEPARATING A GAS MIXTURE BY CRYOGENIC DISTILLATION
JPWO2006011251A1 (en) * 2004-07-30 2008-05-01 三菱重工業株式会社 Refrigerator and air refrigerant cooling system
US20070101756A1 (en) 2004-07-30 2007-05-10 Mitsubishi Heavy Industries, Ltd. Air-refrigerant cooling apparatus
EP1801518B1 (en) * 2004-07-30 2013-09-11 Mitsubishi Heavy Industries, Ltd. Air refrigerant type cooling apparatus and air refrigerant cold system using the same
DE602004025158D1 (en) * 2004-11-29 2010-03-04 Mitsubishi Heavy Ind Ltd AIR COOLING COOLING / HEATER
EP1828693B1 (en) * 2004-12-20 2008-04-02 Angelantoni Industrie SpA Energy-saving climatic test chamber and method of operation
US7225637B2 (en) * 2004-12-27 2007-06-05 L'Air Liquide Société Anonyme á´ Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Integrated air compression, cooling, and purification unit and process
US8375719B2 (en) * 2005-05-12 2013-02-19 Recurrent Engineering, Llc Gland leakage seal system
US8161771B2 (en) * 2007-09-20 2012-04-24 Praxair Technology, Inc. Method and apparatus for separating air
AU2008321326B2 (en) * 2007-11-12 2013-04-18 Exxonmobil Upstream Research Company Methods of generating and utilizing utility gas
US8429933B2 (en) * 2007-11-14 2013-04-30 Praxair Technology, Inc. Method for varying liquid production in an air separation plant with use of a variable speed turboexpander
BRPI0911224A2 (en) * 2008-04-30 2015-09-29 Exxonmobil Upstream Res Co system and method for treating a gaseous feed stream, and structured adsorbent contactor
US8004102B2 (en) * 2009-04-03 2011-08-23 Praxair Technology, Inc. Refrigeration generation method and system
KR101603218B1 (en) * 2010-03-16 2016-03-15 한화테크윈 주식회사 Turbine system
US9067168B2 (en) 2010-05-28 2015-06-30 Exxonmobil Upstream Research Company Integrated adsorber head and valve design and swing adsorption methods related thereto
TWI495501B (en) 2010-11-15 2015-08-11 Exxonmobil Upstream Res Co Kinetic fractionators, and cycling processes for fractionation of gas mixtures
JP6035553B2 (en) 2011-03-01 2016-11-30 エクソンモービル アップストリーム リサーチ カンパニー Method and related apparatus and system for removing contaminants from hydrocarbon streams by swing adsorption
CA2824162A1 (en) 2011-03-01 2012-09-07 Exxonmobil Upstream Research Company Apparatus and systems having a rotary valve assembly and swing adsorption processes related thereto
EA026118B1 (en) 2011-03-01 2017-03-31 Эксонмобил Апстрим Рисерч Компани Method of removing contaminants from a hydrocarbon stream by swing adsorption process and apparatus and system related to this method
US9162175B2 (en) 2011-03-01 2015-10-20 Exxonmobil Upstream Research Company Apparatus and systems having compact configuration multiple swing adsorption beds and methods related thereto
US9017457B2 (en) 2011-03-01 2015-04-28 Exxonmobil Upstream Research Company Apparatus and systems having a reciprocating valve head assembly and swing adsorption processes related thereto
SG192572A1 (en) 2011-03-01 2013-09-30 Exxonmobil Upstream Res Co Apparatus and systems having an encased adsorbent contactor and swing adsorption processes related thereto
CA2842928A1 (en) 2011-03-01 2012-11-29 Exxonmobil Upstream Research Company Apparatus and systems having a rotary valve assembly and swing adsorption processes related thereto
US9957892B2 (en) * 2012-06-20 2018-05-01 Daniel POMERLEAU Jet turbine utilizing a cryogenic fuel
US9034078B2 (en) 2012-09-05 2015-05-19 Exxonmobil Upstream Research Company Apparatus and systems having an adsorbent contactor and swing adsorption processes related thereto
US9118226B2 (en) * 2012-10-12 2015-08-25 Echogen Power Systems, Llc Heat engine system with a supercritical working fluid and processes thereof
US9518778B2 (en) 2012-12-26 2016-12-13 Praxair Technology, Inc. Air separation method and apparatus
EP3149419B1 (en) 2014-06-02 2019-10-30 Praxair Technology, Inc. Air separation system and method
CA2949262C (en) 2014-07-25 2020-02-18 Shwetha Ramkumar Cyclical swing absorption process and system
US10307749B2 (en) 2014-11-11 2019-06-04 Exxonmobil Upstream Research Company High capacity structures and monoliths via paste imprinting
CA2970286C (en) 2014-12-10 2019-08-13 Exxonmobil Research And Engineering Company Adsorbent-incorporated polymer fibers in packed bed and fabric contactors, and methods and devices using same
US9744521B2 (en) 2014-12-23 2017-08-29 Exxonmobil Upstream Research Company Structured adsorbent beds, methods of producing the same and uses thereof
SG11201707069QA (en) 2015-05-15 2017-11-29 Exxonmobil Upstream Res Co Apparatus and system for swing adsorption processes related thereto comprising mid-bed purge systems
CA2979870C (en) 2015-05-15 2019-12-03 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes related thereto
US10293298B2 (en) 2015-09-02 2019-05-21 Exxonmobil Upstream Research Company Apparatus and system for combined temperature and pressure swing adsorption processes related thereto
US10220345B2 (en) 2015-09-02 2019-03-05 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes related thereto
JP6616011B2 (en) 2015-10-27 2019-12-04 エクソンモービル アップストリーム リサーチ カンパニー Apparatus and system for swing adsorption process with multiple valves
CN108348837B (en) 2015-10-27 2021-02-19 埃克森美孚上游研究公司 Apparatus having actively controlled feed poppet valves and passively controlled product valves and systems related thereto for swing adsorption processes
US10322365B2 (en) 2015-10-27 2019-06-18 Exxonmobil Upstream Reseach Company Apparatus and system for swing adsorption processes related thereto
US10744449B2 (en) 2015-11-16 2020-08-18 Exxonmobil Upstream Research Company Adsorbent materials and methods of adsorbing carbon dioxide
RU2714063C1 (en) 2016-03-18 2020-02-11 Эксонмобил Апстрим Рисерч Компани Apparatus and system for implementing short-cycle adsorption processes
RU2716686C1 (en) 2016-05-31 2020-03-13 Эксонмобил Апстрим Рисерч Компани Apparatus and system for implementing short-cycle adsorption processes
CN109219476A (en) 2016-05-31 2019-01-15 埃克森美孚上游研究公司 For becoming the device and system of adsorption method
US10434458B2 (en) 2016-08-31 2019-10-08 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes related thereto
KR102215684B1 (en) 2016-09-01 2021-02-19 엑손모빌 업스트림 리서치 캄파니 Swing adsorption method for water removal using 3A zeolite structure
US10328382B2 (en) 2016-09-29 2019-06-25 Exxonmobil Upstream Research Company Apparatus and system for testing swing adsorption processes
CA3045034C (en) 2016-12-21 2021-06-29 Exxonmobil Upstream Research Company Self-supporting structures having active materials
EP3558490B1 (en) 2016-12-21 2022-06-29 ExxonMobil Upstream Research Company Self-supporting structures having foam-geometry structure and active materials
WO2019147516A1 (en) 2018-01-24 2019-08-01 Exxonmobil Upstream Research Company Apparatus and system for temperature swing adsorption
EP3758828A1 (en) 2018-02-28 2021-01-06 ExxonMobil Upstream Research Company Apparatus and system for swing adsorption processes
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BE1027529B1 (en) * 2019-08-29 2021-03-30 Atlas Copco Airpower Nv Device for gas-tight sealing of a movable shaft and compressor or expander device in which such device is used.
US11655910B2 (en) 2019-10-07 2023-05-23 ExxonMobil Technology and Engineering Company Adsorption processes and systems utilizing step lift control of hydraulically actuated poppet valves
EP4045173A1 (en) 2019-10-16 2022-08-24 Exxonmobil Upstream Research Company (EMHC-N1-4A-607) Dehydration processes utilizing cationic zeolite rho
KR102268313B1 (en) * 2019-11-22 2021-06-23 (주)테크니컬코리아 Compressor system and boil-off gas reliquefaction system using the same
CN115103990A (en) * 2020-03-10 2022-09-23 林德有限责任公司 Cryogenic air separation process and air separation unit
CN112112689B (en) * 2020-09-22 2021-09-21 联优机械(常熟)有限公司 ORC waste heat power generation turbo expander and high-speed motor matching structure
CN113865909A (en) * 2021-10-11 2021-12-31 江苏国富氢能技术装备股份有限公司 Performance testing device for refrigeration expander
US20240010351A1 (en) * 2022-07-08 2024-01-11 Raytheon Technologies Corporation Turbo expanders for turbine engines having hydrogen fuel systems

Family Cites Families (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3477239A (en) * 1967-05-16 1969-11-11 Messer Griesheim Gmbh Multistage compression drive in gas separation
FR2122307B1 (en) * 1971-01-19 1975-01-17 Denis Louis
FR2165729B1 (en) * 1971-12-27 1976-02-13 Technigaz Fr
DE2557453C2 (en) * 1975-12-19 1982-08-12 Linde Ag, 6200 Wiesbaden Process for the production of gaseous oxygen
US4670031A (en) * 1985-04-29 1987-06-02 Erickson Donald C Increased argon recovery from air distillation
US4817393A (en) * 1986-04-18 1989-04-04 Erickson Donald C Companded total condensation loxboil air distillation
US4769055A (en) * 1987-02-03 1988-09-06 Erickson Donald C Companded total condensation reboil cryogenic air separation
DE4109945A1 (en) * 1991-03-26 1992-10-01 Linde Ag METHOD FOR DEEP TEMPERATURE DISPOSAL OF AIR
US5402631A (en) * 1991-05-10 1995-04-04 Praxair Technology, Inc. Integration of combustor-turbine units and integral-gear pressure processors
US5289688A (en) * 1991-11-15 1994-03-01 Air Products And Chemicals, Inc. Inter-column heat integration for multi-column distillation system
FR2702040B1 (en) * 1993-02-25 1995-05-19 Air Liquide Process and installation for the production of oxygen and / or nitrogen under pressure.
US5363657A (en) * 1993-05-13 1994-11-15 The Boc Group, Inc. Single column process and apparatus for producing oxygen at above-atmospheric pressure
GB9404991D0 (en) * 1994-03-15 1994-04-27 Boc Group Plc Cryogenic air separation
US5467613A (en) * 1994-04-05 1995-11-21 Carrier Corporation Two phase flow turbine
US5460003A (en) * 1994-06-14 1995-10-24 Praxair Technology, Inc. Expansion turbine for cryogenic rectification system
US5711167A (en) * 1995-03-02 1998-01-27 Air Liquide Process & Construction High efficiency nitrogen generator
US5582034A (en) * 1995-11-07 1996-12-10 The Boc Group, Inc. Air separation method and apparatus for producing nitrogen
US5582033A (en) * 1996-03-21 1996-12-10 Praxair Technology, Inc. Cryogenic rectification system for producing nitrogen having a low argon content
US5689973A (en) * 1996-05-14 1997-11-25 The Boc Group, Inc. Air separation method and apparatus

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104018891A (en) * 2014-05-23 2014-09-03 武汉船用机械有限责任公司 Steam turbine
CN104018891B (en) * 2014-05-23 2016-03-09 武汉船用机械有限责任公司 A kind of steam turbine
CN112066643A (en) * 2020-07-28 2020-12-11 上海加力气体有限公司 Air separation process with reduced energy consumption

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EP0880000A2 (en) 1998-11-25
KR19980087144A (en) 1998-12-05
EP0880000A3 (en) 1998-12-16
CA2237830C (en) 2002-10-22
CN1138961C (en) 2004-02-18
US5924307A (en) 1999-07-20
BR9801656A (en) 1999-09-14
CA2237830A1 (en) 1998-11-19

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